Reforming catalyst for hydrocarbon, method for producing hydrogen using such reforming catalyst, and fuel cell system

ABSTRACT

A hydrocarbon reforming catalyst which maintains carrier strength even after a long-term thermal history and which exhibits high catalytic activity is prepared by causing at least one noble metal component selected from among a ruthenium component, a platinum component, a rhodium component, a palladium component, and an iridium component to be supported on a carrier containing manganese oxide, alumina, and at least one compound selected from among lanthanum oxide, cerium oxide, and zirconium oxide, or a carrier containing silicon oxide, manganese oxide, and alumina. By use of the reforming catalyst, hydrogen is produced through steam reforming (1), autothermal reforming (2), partial-oxidation reforming (3), or carbon dioxide reforming (4). A fuel cell system is constituted from a reformer employing the reforming catalyst, and a fuel cell employing, as a fuel, hydrogen produced by the reformer.

TECHNICAL FIELD

The present invention relates to a catalyst for use in reforming ofhydrocarbon (hereinafter referred to as a hydrocarbon reformingcatalyst), to a method for producing hydrogen by use of the reformingcatalyst, and to a fuel cell system. More particularly, the inventionrelates to a hydrocarbon reforming catalyst comprising a carriercontaining at least one compound selected from among lanthanum oxide,cerium oxide, and zirconium oxide; manganese oxide; and alumina, or acarrier containing silicon oxide, manganese oxide, and alumina, and,supported on the carrier, at least one noble metal component selectedfrom among a ruthenium component, a platinum component, a rhodiumcomponent, a palladium component, and an iridium component, the catalystexhibiting enhanced catalytic activity, durability (compressivestrength), and heat resistance (prevention of decrease in surface areaand strength); to a method for producing hydrogen by use of thereforming catalyst; and to a fuel cell system employing the reformingcatalyst.

BACKGROUND ART

In recent years, new energy-production techniques have attractedattention from the standpoint of environmental issues, and among thesetechniques a fuel cell has attracted particular interest. The fuel cellconverts chemical energy to electric energy through electrochemicalreaction of hydrogen and oxygen, attaining high energy utilizationefficiency. Therefore, extensive studies have been carried out onrealization of fuel cells for public use, industrial use, automobileuse, etc.

Fuel cells are categorized in accordance with the type of employedelectrolyte, and, among others, a phosphoric acid type, a moltencarbonate salt type, a solid oxide type, and a polymer electrolyte typehave been known. With regard to hydrogen sources, studies have beenconducted on methanol; liquefied natural gas predominantly containingmethane; city gas predominantly containing natural gas; a syntheticliquid fuel produced from natural gas serving as a feedstock; andpetroleum-derived hydrocarbons such as naphtha and kerosene.

When hydrogen is produced from petroleum-derived hydrocarbons, thehydrocarbons are generally steam-reformed in the presence of a catalyst.Among such catalysts, catalysts that contain ruthenium supported on acarrier as an active component have conventionally been studied, in viewof their advantages; e.g., comparatively high activity and suppressionof carbon deposition even under low steam/carbon ratio operationalconditions. In recent years, these ruthenium catalysts have beenenvisaged for use in fuel cells, which require a long-life catalyst.

Since the discovery of a co-catalyst effect of cerium oxide or zirconiumoxide exerted on a ruthenium catalyst, ruthenium-cerium oxide-based andruthenium-zirconium oxide-based catalysts have been studied and somepatent applications have been filed. In addition to ruthenium-basedcatalysts, catalysts based on a platinum component, a rhodium component,a palladium component, an iridium component, or a nickel component havebeen studied. However, these catalysts have drawbacks, in that catalyticactivity in terms of steam reforming of hydrocarbons remainsunsatisfactory, and that carbon is deposited in a large amount duringreforming.

In addition to the aforementioned steam reforming, other reformingprocesses for producing hydrogen, such as autothermal reforming,partial-oxidation reforming, and carbon dioxide reforming have beenstudied. As is known, all the above reforming processes can generally beperformed through employment of the same reforming catalyst, and withslight modification of reforming conditions, all the above processes canalso produce synthesis gas. Studies have also been carried out on use ofcomponents such as a ruthenium component, a platinum component, arhodium component, a palladium component, an iridium component, and anickel component in catalysts for the above autothermal reforming,partial-oxidation reforming, and carbon dioxide reforming. However,catalytic activity of the catalyst employing the elements remainsunsatisfactory.

There have been proposed an enhanced-activity hydrocarbon reformingcatalyst comprising a carrier containing manganese oxide and, supportedon the carrier, at least one component selected from among a rutheniumcomponent, a platinum component, a rhodium component, a palladiumcomponent, an iridium component, and a nickel component; a method forproducing the reforming catalyst; and methods of the steam reforming,autothermal reforming, partial-oxidation reforming, and carbon dioxidereforming of hydrocarbon by use of the reforming catalyst (PatentDocument 1).

There have been proposed a hydrocarbon reforming catalyst which isproduced by preparing a catalyst comprising a carrier containingmanganese oxide and, supported on the carrier, at least one componentselected from among a ruthenium component, a platinum component, arhodium component, a palladium component, an iridium component, and anickel component, by use of at least one chlorine-containing compound;decomposing the compound with an aqueous alkaline solution, and removingchlorine atoms through washing with water; a method for producing thecatalyst; and a hydrocarbon reforming method employing the reformingcatalyst (Patent Document 2). However, the above disclosed reformingcatalysts, exhibiting high activity in terms of reforming reaction, haveproblematically poor durability; i.e., poor strength, particularlycompressive strength.

Patent Document 1

Pamphlet of International Patent Application No. 02/078840

Patent Document 2

Japanese Patent Application Laid-Open (kokai) No. 2003-265963

DISCLOSURE OF THE INVENTION

The present invention has been conceived under such circumstances, andan object of the present invention is to provide a hydrocarbon reformingcatalyst which maintains carrier strength (particularly, compressivestrength of the carrier) and heat resistance even after a long-termthermal history, which exhibits high catalytic activity, and whichmaintains the catalytic activity even after a long-term thermal history.Another object is to provide a hydrocarbon reforming catalyst whichexhibits enhanced heat resistance (i.e., prevention of decrease insurface area and strength). Still another object is to provide a methodfor producing hydrogen by use of any of the reforming catalysts.

Yet another object of the invention is to provide an advanced fuel cellsystem comprising a reformer employing such an excellent reformingcatalyst, and a fuel cell employing, as a fuel, hydrogen produced by thereformer.

The present inventors have carried out extensive studies in an effort toattain the aforementioned objects, and have found that through use of acarrier containing manganese oxide and alumina and, as an additive, atleast one compound selected from among lanthanum oxide, cerium oxide,and zirconium oxide, surface diffusion of alumina and α phase nucleationare prevented, thereby maintaining strength of the carrier even after along-term thermal history, and a ruthenium component, a platinumcomponent, a rhodium component, a palladium component, or an iridiumcomponent is supported on the carrier in a highly dispersed state,whereby activity of the produced reforming catalyst increases and ismaintained after a long-term thermal history. The inventors have alsofound that through use of a carrier containing manganese oxide andalumina and, as an additive, silicon oxide, a reforming catalyst inwhich a ruthenium component, a platinum component, a rhodium component,a palladium component, or an iridium component is supported on thecarrier exhibits enhanced heat resistance. The present invention hasbeen accomplished on the basis of these findings.

The present invention is directed to the following.

(1) A hydrocarbon reforming catalyst comprising a carrier containing atleast one compound (a) selected from among lanthanum oxide, ceriumoxide, and zirconium oxide, manganese oxide (b), and alumina (c), and,supported on the carrier, at least one noble metal component (d)selected from among a ruthenium component, a platinum component, arhodium component, a palladium component, and an iridium component.(2) The hydrocarbon reforming catalyst as described in (1) above,wherein the carrier is produced by impregnating an alumina (c) with atleast one compound (a′) selected from among a lanthanum compound, acerium compound, and a zirconium compound, and a manganese compound(b′), and calcining the impregnated alumina carrier.(3) The hydrocarbon reforming catalyst as described in (2) above, whichis produced through calcining at 800 to 1,000° C.(4) The hydrocarbon reforming catalyst as described in (1) above,wherein the carrier is produced by impregnating alumina (c) with atleast one compound (a′) selected from among a lanthanum compound, acerium compound, and a zirconium compound; calcining the impregnatedalumina carrier at 400 to 600° C.; impregnating the calcined carrierwith a manganese compound (b′); and calcining the thus-impregnatedcarrier at 800 to 1,000° C.(5). The hydrocarbon reforming catalyst as described in (1) above,wherein the amount of at least one compound selected from amonglanthanum oxide, cerium oxide, and zirconium oxide is 1 to 20 mass %with respect to that of the reforming catalyst.(6). A hydrocarbon reforming catalyst comprising a carrier containingsilicon oxide (f), manganese oxide (b), and alumina (c), and, supportedon the carrier, at least one noble metal component (d) selected fromamong a ruthenium component, a platinum component, a rhodium component,a palladium component, and an iridium component.(7). The hydrocarbon reforming catalyst as described in (6) above,wherein the carrier is produced by impregnating alumina (c) with asilicon compound (f′) and calcining the impregnated alumina, and,subsequently, impregnating the calcined alumina with a manganesecompound (b′) and calcining the thus-impregnated alumina.(8). The hydrocarbon reforming catalyst as described in (6) above,wherein the carrier is produced by impregnating alumina (c) with amanganese compound (b′) and calcining the impregnated alumina, and,subsequently impregnating the calcined alumina with a silicon compound(f′) and calcining the thus-impregnated alumina.(9). The hydrocarbon reforming catalyst as described in (6) above,wherein the carrier is produced by mixing a manganese compound (b′) anda silicon compound (f′), impregnating alumina (c) simultaneously withthe compounds, and calcining the impregnated alumina.(10). The hydrocarbon reforming catalyst as described in any one of (6)to (9) above, wherein the silicon compound (f′) is tetraethoxysilane.(11). The hydrocarbon reforming catalyst as described in any one of (6)to (10) above, which has a silicon oxide (f) content of 1 to 20 mass %.(12). The hydrocarbon reforming catalyst as described in any one of (1)to (11) above, wherein the manganese compound (b′) is manganese acetate.(13). The hydrocarbon reforming catalyst as described in (1) or (6)above, wherein said at least one noble metal component selected fromamong a ruthenium component, a platinum component, a rhodium component,a palladium component, and an iridium component is contained in thereforming catalyst in an amount of 0.1 to 8 mass % as reduced to noblemetal element(s).(14). The hydrocarbon reforming catalyst as described in (1) or (6)above, wherein the manganese oxide (b) is contained in the reformingcatalyst in an amount of 3 to 20 mass %.(15). The hydrocarbon reforming catalyst as described in any one of (1)to (14) above, which further contains at least one species selected froman alkali metal component and an alkaline earth metal component.(16). A method for producing hydrogen, characterized by comprisingreforming of hydrocarbon by use of a reforming catalyst as recited inany one of (1) to (15).(17). The method for producing hydrogen as described in (16) above,wherein the reforming is steam reforming, autothermal reforming,partial-oxidation reforming, or carbon dioxide reforming.(18). A fuel cell system, characterized by comprising a reformeremploying a reforming catalyst as recited in any one of (1) to (15)above, and a fuel cell employing, as a fuel, hydrogen produced by thereformer.

According to the present invention, there can be provided a hydrocarbonreforming catalyst which maintains carrier strength (particularly,compressive strength of the carrier) even after a long-term thermalhistory, which exhibits high catalytic activity, and which maintains thecatalytic activity even after a long-term thermal history; a hydrocarbonreforming catalyst which exhibits enhanced heat resistance; and a methodfor producing hydrogen by use of any of the reforming catalysts. Theinvention can also provide an advanced fuel cell system comprising areformer employing such an excellent reforming catalyst, and a fuel cellemploying, as a fuel, hydrogen produced by the reformer.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic configuration of an embodiment of the fuel cellsystem of the present invention.

DESCRIPTION OF THE REFERENCE NUMERALS

-   1: Vaporizer-   11: Water-feeding pipe-   12: Fuel conduit-   15: Connecting pipe-   21: Fuel tank-   22: Fuel pump-   23: Desulfurizer-   24: Water pump-   31: Reformer-   31A: Burner of reformer-   32: Shift reactor of carbon monoxide-   33: Preferential oxidation reactor of carbon monoxide-   34: Fuel cell-   34A: Fuel cell negative electrode-   34B: Fuel cell positive electrode-   34C: Fuel cell polymer electrolyte-   35: Air blower-   36: Gas-water separator-   37: Exhaust heat recovery unit-   37A: Heat exchanger-   37B: Heat exchanger-   37C: Cooling unit-   37D: Cooling medium circulation pump

BEST MODE FOR CARRYING OUT THE INVENTION

The present invention will next be described in detail.

The hydrocarbon reforming catalyst of the present invention includes acarrier containing at least one compound (a) selected from amonglanthanum oxide, cerium oxide, and zirconium oxide, manganese oxide (b),and alumina (c), and, supported on the carrier, at least one noble metalcomponent (d) selected from among a ruthenium component, a platinumcomponent, a rhodium component, a palladium component, and an iridiumcomponent. Alternatively, the hydrocarbon reforming catalyst of thepresent invention includes a carrier containing silicon oxide (f),manganese oxide (b), and alumina (c), and, supported on the carrier, atleast one noble metal component (d) selected from among a rutheniumcomponent, a platinum component, a rhodium component, a palladiumcomponent, and an iridium component.

The above reforming catalyst and the production method therefor willnext be described.

The method for producing a reforming catalyst including preparing acarrier containing at least one compound selected from among lanthanumoxide, cerium oxide, and zirconium oxide, manganese oxide, and aluminawill now be described. One exemplary method is as follows.

(i) Specifically, at least one compound selected from among a lanthanumcompound (e.g., lanthanum nitrate), a cerium compound (e.g., ceriumnitrate), and a zirconium compound (e.g., zirconium nitrate) isdissolved in water, and alumina is impregnated with the solution. (ii)The thus-impregnated alumina is dried by means of a dryer at about 100to 200° C. for about 1 to 10 hours, and calcined in a heating furnace atabout 400 to 600° C., preferably about 500° C., for about 1 to 10 hours,preferably about 2 to 5 hours, whereby an alumina carrier containing atleast one compound selected from among lanthanum oxide, cerium oxide,and zirconium oxide is prepared. (iii) Subsequently, a manganesecompound (e.g., manganese acetate) is dissolved in water, and thealumina carrier containing at least one compound selected from amonglanthanum oxide, cerium oxide, and zirconium oxide produced in (ii)above is impregnated with the solution. (iv) The thus-impregnatedalumina carrier is dried by means of a dryer at about 100 to 200° C. forabout 1 to 10 hours, and calcined in a heating furnace at about 800 to1,000° C., preferably about 800° C., for about 1 to 10 hours, preferablyabout 2 to 5 hours, whereby a carrier containing at least one compoundselected from among lanthanum oxide, cerium oxide, and zirconium oxide,manganese oxide, and alumina is prepared. (v) At least one noble metalcomponent selected from among a ruthenium component, a platinumcomponent, a rhodium component, a palladium component, and an iridiumcomponent is dissolved in water, and the carrier prepared in (iv) aboveis impregnated with the solution. (vi) Subsequently, the impregnationproduct is dried naturally or by means of a dryer such as a rotaryevaporator or a blower dryer for about 30 to 180 minutes. (vii) Then,the catalyst precursor prepared in (vi) above is impregnated with anaqueous (about 1 to 10 mol/L) sodium hydroxide solution for severalhours, to thereby decompose compounds supported on the carrier. (viii)Subsequently, the product of (vii) above is sufficiently washed withdistilled water or the like and dried by means of, for example, a dryerat about 100 to 200° C. for about 1 to 10 hours, whereby a reformingcatalyst of interest is produced.

Another embodiment of the production method is as follows. Specifically,(ix) a manganese compound (e.g., manganese acetate) is dissolved inwater, and alumina is impregnated with the solution. (x) Theimpregnation product is dried by means of a dryer at about 100 to 200°C. for about 1 to 10 hours, and calcined in a heating furnace at about800 to 1,000° C., preferably about 800° C., for about 1 to 10 hours,preferably about 2 to 5 hours, whereby an alumina carrier containingmanganese oxide is prepared. (xi) Subsequently, at least one compoundselected from among a lanthanum compound (e.g., lanthanum nitrate), acerium compound (e.g., cerium nitrate), and a zirconium compound (e.g.,zirconium nitrate) is dissolved in water. (xii) Themanganese-oxide-containing aluminum carrier prepared in (x) above isimpregnated with the solution. (xiii) Subsequently, the impregnationproduct is dried by means of a dryer at about 100 to 200° C. for about 1to 10 hours, and calcined in a heating furnace at about 800 to 1,000°C., preferably about 800° C., for about 1 to 10 hours, preferably about2 to 5 hours, whereby a carrier containing alumina, manganese oxide, andat least one compound selected from among lanthanum oxide, cerium oxide,and zirconium oxide is prepared.

(xiv) Subsequently, the steps as described in (v) to (viii) above aresequentially carried out, whereby a reforming catalyst of interest isproduced.

Still another embodiment of the production method is as follows.Specifically, a manganese compound (e.g., manganese acetate) and atleast one compound selected from among a lanthanum compound (e.g.,lanthanum nitrate), a cerium compound (e.g., cerium nitrate), and azirconium compound (e.g., zirconium nitrate) are dissolved in water, andalumina is impregnated with the solution. Subsequently, the impregnationproduct is dried by means of a dryer at about 100 to 200° C. for about 1to 10 hours, and calcined in a heating furnace at about 800 to 1,000°C., preferably about 800° C., for about 1 to 10 hours, preferably about2 to 5 hours, whereby a carrier containing alumina, manganese oxide, andat least one compound selected from among lanthanum oxide, cerium oxide,and zirconium oxide is prepared. Subsequently, the steps as described in(v) to (viii) above are sequentially carried out, whereby a reformingcatalyst of interest is produced.

The method for producing a hydrocarbon reforming catalyst including acarrier containing silicon oxide, manganese oxide, and alumina and,supported on the carrier, at least one noble metal component selectedfrom among a ruthenium component, a platinum component, a rhodiumcomponent, a palladium component, and an iridium component will now bedescribed. One exemplary method is as follows. (A) Specifically, asilicon compound (e.g., tetraethoxysilane) is dissolved in ethanol, andalumina is immersed in the solution. The mixture is allowed to react at30 to 80° C. for about 1 to 5 hours with stirring. (B) After completionof reaction, ethanol is evaporated, and the residue is dried by means ofa dryer at about 100 to 200° C. for about 5 to 20 hours, and calcined ina heating furnace at about 800 to 1,000° C., preferably about 800° C.,for about 1 to 10 hours, preferably about 3 to 5 hours, whereby analumina carrier containing silicon oxide is prepared. (C) Subsequently,a manganese compound (e.g., manganese acetate) is dissolved in water,and the silicon-oxide-containing alumina carrier prepared in (A) aboveis impregnated with the solution. The impregnation product is dried bymeans of a dryer at about 100 to 200° C. for about 5 to 20 hours, andcalcined in a heating furnace at about 800 to 1,000° C., preferablyabout 800° C., for about 1 to 10 hours, preferably about 3 to 5 hours,whereby an alumina carrier containing silicon oxide and manganese oxideis produced.

Another embodiment of the production method is as follows. (D) Firstly,a manganese compound (e.g., manganese acetate) is dissolved in water,and alumina is impregnated with water. The impregnation product is driedby means of a dryer at about 100 to 200° C. for about 5 to 20 hours. (E)Subsequently, a silicon compound (e.g., tetraethoxysilane) is dissolvedin ethanol, and the impregnation product is immersed in the ethanolsolution. The mixture is allowed to react at 30 to 80° C. for about 1 to5 hours with stirring. (F) After completion of reaction, ethanol isevaporated, and the residue is dried by means of a dryer at about 100 to200° C. for about 5 to 20 hours, and calcined in a heating furnace atabout 800 to 1,000° C., preferably about 800° C., for about 1 to 10hours, preferably about 3 to 5 hours, whereby an alumina carriercontaining silicon oxide and manganese oxide is prepared.

In still another embodiment, a silicon compound (e.g.,tetraethoxysilane) dissolved in ethanol and a manganese compound (e.g.,manganese acetate) dissolved in water are provided, and two solutionsare mixed with stirring. Alumina is impregnated with the solutionmixture. The impregnation product is dried by means of a dryer at about100 to 200° C. for about 5 to 20 hours, and calcined in a heatingfurnace at about 800 to 1,000° C., preferably about 800° C., for about 1to 10 hours, preferably about 3 to 5 hours, whereby an alumina carriercontaining silicon oxide and manganese oxide is prepared.

The thus-produced alumina carrier containing silicon oxide and manganeseoxide is impregnated with an aqueous solution containing at least onenoble metal component selected from among a ruthenium component, aplatinum component, a rhodium component, a palladium component, and aniridium component. The impregnation product is dried naturally or bymeans of a dryer such as a rotary evaporator or a blower dryer for about30 to 180 minutes. Then, the dried product is impregnated with anaqueous (about 1 to 10 mol/L) sodium hydroxide solution for severalhours, to thereby decompose compounds supported on the carrier.Subsequently, the product is sufficiently washed with distilled water orthe like, and water is removed through filtration or a similar means,followed by drying by means of, for example, a dryer at about 100 to200° C. for about 1 to 10 hours, whereby a reforming catalyst ofinterest is produced.

In the present invention, manganese oxides having a variety of valencesmay be employed, and specific examples include MnO, Mn₃O₄, Mn₂O₃, MnO₂,MnO₃, and Mn₂O₇. Of these, tetravalent manganese dioxide (MnO₂) ispreferred from the viewpoint of availability and stability. A commercialmanganese dioxide (MnO₂) product may be employed, and manganese dioxide(MnO₂) produced through calcining a manganese compound such as manganeseacetate [Mn(CH₃COO)₂.4H₂O], manganese sulfate [MnSO₄.5H₂O], manganesenitrate [Mn(NO₃)₂.6H₂O], or manganese chloride [MnCl₂.4H₂O] may also beemployed.

The manganese oxide content is preferably 3 to 20 mass % based on thereforming catalyst, more preferably 5 to 15 mass %.

The alumina species which forms the carrier may be commercial productshaving any crystal type; i.e., α, β, γ, η, θ, κ, or χ. Of these,α-alumina, alumina having an α-alumina phase, and γ-alumina arepreferred from the viewpoint of catalytic activity.

As the alumina species, alumina hydrate (e.g., boehmite, bialite, orgibbsite) calcined product may also be employed. Alternatively, theremay be employed alumina produced by calcining aluminum hydroxideprecipitates which have been formed by adding an alkaline buffer (pH: 8to 10) to aluminum nitrate. A calcined product of aluminum chloride mayalso be used. Yet alternatively, alumina prepared through the solgelmethod may also be employed. Specifically, an alkoxide such as aluminumisopropoxide is dissolved in an alcohol such as 2-propanol, and aluminagel is prepared from the solution in the presence of inorganic acid(e.g., hydrochloric acid) serving as a hydrolysis catalyst. The gel isdried and calcined, to thereby form alumina.

Upon use of manganese oxide and alumina in combination, alumina andmanganese oxide may be mixed for use. In an alternative manner, aluminais impregnated with an aqueous solution of a manganese compound such asmanganese acetate [Mn(CH₃COO)₂.4H₂O], manganese sulfate [MnSO₄.5H₂O],manganese nitrate [Mn(NO₃)₂.6H₂O], or manganese chloride [MnCl₂.4H₂O],and the impregnation product is calcined.

The lanthanum compound employed in the present invention is preferablyhighly water-soluble. Examples of such compounds include lanthanumchloride (LaCl₃, LaCl₃.7H₂O), lanthanum bromide (LaBr₃), lanthanumiodide (LaI₃), lanthanum nitrate [La(NO₃)₃.6H₂O], and lanthanum acetate[La(CH₃COO)₃.1.5H₂O].

Cerium compounds are present in a valence state of three or four. In thepresent invention, a trivalent cerium compound is preferably used fromthe viewpoint of stability. Examples of such compounds include ceriumchloride (CeCl₃), cerium bromide (CeBr₃), cerium iodide (CeI₃), ceriumnitrate [Ce(NO₃)₃.6H₂O], cerium carbonate [Ce₂(CO₃)₃.5H₂O], and ceriumsulfate [Ce₂(SO₄)₃.nH₂O].

Zirconium compounds are present in a valence state of two, three, orfour. Examples of such compounds include zirconium chloride (ZrCl₂,ZrCl₃, ZrCl₄), zirconium bromide (ZrBr₂, ZrBr₃, ZrBr₄), zirconium iodide(ZrI₂, ZrI₃, ZrI₄), zirconium nitrate [Zr(NO₃)₂.2H₂O], zirconia nitrate[ZrO(NO₃)₂.H₂O], zirconium sulfate [Zr(SO₄)₂, Zr(SO₄)₂.4H₂O], zirconiumacetate [Zr(CH₃CO₂)₄], and zirconia acetate [ZrO(CH₃CO₂)₂].

The silicon compound employable in the present invention may be anorganic silane compound, which is readily dissolved in organic solventsuch as ethanol and which has high storage stability. Preferably, thesilicon compound has no halogen atom such as a chlorine atom. Thus,tetraalkoxysilane is preferably employed. Examples of thetetraalkoxysilane include tetramethoxysilane, tetraethoxysilane,tetrapropoxysilane, and tetrabutoxysilane.

When alumina is impregnated with an aqueous solution of theaforementioned manganese compound, lanthanum compound, cerium compound,or zirconium compound for incorporating a catalyst component into thecarrier, the amount of water for preparing the aqueous solution of eachcompound is preferably adjusted such that the dissolution water ratiofalls within a range of 0.7 to 1.3.

The aforementioned dissolution water ratio is calculated according tothe following formula (1):Dissolution water ratio=volume of water employed (mL)/volume ofdissolution water required (mL)  (1).

The volume of water employed includes not only water for preparing asolution but also water of crystallization contained in the manganesecompound, lanthanum compound, cerium compound, or zirconium compound.The volume of dissolution water required refers to water absorptioncapacity of the alumina carrier, and is calculated according to thefollowing formula (2):Volume of dissolution water required (mL)=micropore volume of carrier(mL/g)×amount of carrier (g)  (2)(wherein the miropore volume of the alumina carrier has been determinedthrough mercury penetration method). The micropore volume of thealuminum carrier employed in the present invention (KHO-24, product ofSumitomo Chemical Co., Ltd.) was determined to be 0.42 mL/g.

When the carrier is impregnated with a manganese compound, a lanthanumcompound, a cerium compound, or a zirconium compound in a dividedmanner, the dissolution water ratio is preferably adjusted to 0.7 to 1.3in each impregnation operation.

Generally, the aforementioned alumina containing a manganese compoundand at least one species selected from among a lanthanum compound, acerium compound, and a zirconium compound, which has been supportedthereon, is preferably calcined at 800 to 1,000° C. from the viewpointof catalytic activity. The calcining atmosphere may be oxygen, air, or,depending on the type of the manganese compound, inert gas such asnitrogen or argon. The gas temperature is preferably 800 to 900° C.Specifically, either alumina serving as a carrier material or aluminacontaining a manganese compound and at least one species selected fromamong a lanthanum compound, a cerium compound, and a zirconium compound,which are supported thereon may be treated at high temperature (800 to1,000° C.). Although both alumina species may be treated at hightemperature, in an economically preferred mode, the alumina species onwhich a manganese compound and at least one species selected from amonga lanthanum compound, a cerium compound, and a zirconium compound havebeen supported thereon is treated at high temperature. When thetreatment temperature falls within a range of 800 to 1,000° C.,catalytic activity can be enhanced, and deterioration of catalyticactivity caused by sintering is prevented.

In the case where only at least one species selected from among alanthanum compound, a cerium compound, and a zirconium compound isincorporated at first into alumina, calcination is performed at about400 to 600° C., preferably about 500° C.

In the case where the alumina on which a manganese compound and asilicon compound have been supported is calcined, when the calciningtemperature falls within a range of 800 to 1,000° C., catalytic activitycan be enhanced, and deterioration of catalytic activity caused bysintering is prevented.

Subsequently, into the carrier containing at least one compound selectedfrom among lanthanum oxide, cerium oxide, and zirconium oxide, manganeseoxide, and alumina, or onto the carrier containing manganese oxide,silicon oxide, and alumina, at least one component (d) selected from aruthenium component, a platinum component, a palladium component, and aniridium component is incorporated. If required, at least one component(e) selected from an alkali metal component and an alkaline earth metalcomponent is further supported on the carriers.

In the above supporting operation, a solution containing component (d)or a solution containing components (d) and (e) is used. Although thesecomponents may be supported in separate steps, economically, they arepreferred to be supported simultaneously.

Supporting may be performed through a variety of methods, for example,impregnation techniques such as heat impregnation, room temperatureimpregnation, vacuum impregnation, atmospheric pressure impregnation,impregnation-dryness method, and pore-filling method; immersion; lightpermeation method; wet adsorption method; spraying method; and coatingmethod. Of these, impregnation techniques are preferred.

Similar to conventional cases, the above supporting operation may beappropriately carried out under atmospheric pressure or reducedpressure. No particular limitation is imposed on the operationtemperature, and the operation may be performed at or near roomtemperature. If required, additional heating or moisturizing may beperformed. For example, the operation may be appropriately performed atroom temperature to about 150° C. The time for contact between thecomponents and the carrier is one minute to 10 hours.

Examples of ruthenium compounds serving as a source of the rutheniumcomponent include RuCl₃.nH₂O, Ru(NO₃)₃, Ru₂(OH)₂Cl₄.7NH₃.3H₂O,K₂(RuCl₅(H₂O)), (NH₄)₂(RuCl₅(H₂O)), K₂(RuCl₅(NO)), RuBr₃.nH₂O, Na₂RuO₄,Ru(NO)(NO₃)₃, (Ru₃O(OAc)₆(H₂O)₃)OAc.nH₂O, K₄(Ru(CN)₆).nH₂O,K₂(Ru(NO₂)₄(OH)(NO)), (Ru(NH₃)₆)Cl₃, (Ru(NH₃)₆)Br₃, (Ru(NH₃)₆)Cl₂,(Ru(NH₃)₆)Br₂, (Ru₃O₂(NH₃)₁₄)Cl₆.H₂O, (Ru(NO)(NH₃)₅)Cl₃,(Ru(OH)(NO)(NH₃)₄)(NO₃)₂, RuCl₂(PPh₃)₃, RuCl₂(PPh₃)₄,(RuClH(PPh₃)₃).C₇H₈, RuH₂(PPh₃)₄, RUClH(CO)(PPh₃)₃, RuH₂(CO)(PPh₃)₃,(RuCl₂(cod))_(n), Ru(CO)₁₂, Ru(acac)₃, (Ru(HCOO)(CO)₂)_(n), andRu₂I₄(p-cymene)₂. These compounds may be used singly or in combinationof two or more species. Of these, RuCl₃.nH₂O, Ru(NO₃)₃, andRu₂(OH)₂Cl₄.7NH₃.3H₂O are preferably used from the viewpoint of easinessin handling, with RuCl₃.nH₂O being particularly preferred.

Examples of platinum compounds serving as a source of the platinumcomponent include PtCl₄, H₂PtCl₆, Pt(NH₃)₄Cl₂, (NH₄)₂PtCl₂, H₂PtBr₆,NH₄[Pt(C₂H₄)Cl₃], Pt(NH₃)₄(OH)₂, and Pt(NH₃)₂(NO₂)₂. These compounds maybe used singly or in combination of two or more species.

Examples of rhodium compounds serving as a source of the rhodiumcomponent include Na₃RhCl₆, (NH₄)₂RhCl₆, Rh(NH₃)₅Cl₃, and RhCl₃. Thesecompounds may be used singly or in combination of two or more species.

Examples of palladium compounds serving as a source of the palladiumcomponent include (NH₄)₂PdCl₆, (NH₄)₂PdCl₄, Pd(NH₃)₄Cl₂, PdCl₂, andPd(NO₃)₂. These compounds may be used singly or in combination of two ormore species.

Examples of iridium compounds serving as a source of the iridiumcomponent include (NH₄)₂IrCl₆, IrCl₃, and H₂IrCl₆. These compounds maybe used singly or in combination of two or more species.

Examples of alkali metal components preferably employed in the inventioninclude potassium, cesium, rubidium, sodium, and lithium.

Examples of compounds serving as a source of the alkali metal componentinclude K salts such as K₂B₁₀O₁₆, KBr, KBrO₃, KCN, K₂CO₃, KCl, KClO₃,KClO₄, KF, KHCO₃, KHF₂, KH₂PO₄, KH₅(PO₄)₂, KHSO₄, KI, KIO₃, KIO₄,K₄I₂O₉, KN₃, KNO₂, KNO₃, KOH, KPF₆, K₃PO₄, KSCN, K₂SO₃, K₂SO₄, K₂S₂O₃,K₂S₂O₅, K₂S₂O₆, K₂S₂O₈, and K(CH₃COO); Cs salts such as CsCl, CsClO₃,CsClO₄, CsHCO₃, CsI, CsNO₃, Cs₂SO₄, Cs(CH₃COO), CS₂CO₃, and CsF; Rbsalts such as Rb₂B₁₀O₁₆, RbBr, RbBrO₃, RbCl, RbClO₃, RbClO₄, RbI, RbNO₃,Rb₂SO₄, Rb(CH₃COO), and Rb₂CO₃; Na salts such as Na₂B₄O₇, NaB₁₀O₁₆,NaBr, NaBrO₃, NaCN, Na₂CO₃, NaCl, NaClO, NaClO₃, NaClO₄, NaF, NaHCO₃,NaH₂PO₃, Na₂HPO₃, Na₂HPO₄, NaH₂PO₄, Na₃HP₂O₆, Na₂H₂P₂O₇, NaI, NaIO₃,NaIO₄, NaN₃, NaNO₂, NaNO₃, NaOH, Na₂PO₃, Na₃PO₄, Na₄P₂O₇, Na₂S, NaSCN,Na₂SO₃, Na₂SO₄, Na₂S₂O₅, Na₂S₂O₆, and Na(CH₃COO); and Li salts such asLiBO₂, Li₂B₄O₇, LiBr, LiBrO₃, Li₂CO₃, LiCl, LiClO₃, LiClO4, LiHCO₃,Li₂HPO₃, LiI, LiN₃, LiNH₄SO₄, LiNO₂, LiNO₃, LiOH, LiSCN, Li₂SO₄, andLi₃VO₄. These compounds may be used singly or in combination or two ormore species.

Examples of alkaline earth metal components preferably employed in theinvention include barium, calcium, magnesium, and strontium.

Examples of compounds serving as a source of the alkali metal componentinclude Ba salts such as BaBr₂, Ba(BrO₃)₂, BaCl₂, Ba(ClO₂)₂, Ba(ClO₃)₂,Ba(ClO₄)₂, BaI₂, Ba(N₃)₂, Ba(NO₂)₂, Ba(NO₃)₂, Ba(OH)₂, BaS, BaS₂O₆,BaS₄O₆, and Ba(SO₃NH₂)₂; Ca salts such as CaBr₂, CaI₂, CaCl₂, Ca(ClO₃)₂,Ca(IO₃)₂, Ca(NO₂)₂, Ca(NO₃)₂, CaSO₄, CaS₂O₃, CaS₂O₆, Ca(SO₃NH₂)₂,Ca(CH₃COO)₂, and Ca(H₂PO₄)₂; Mg salts such as MgBr₂, MgCO₃, MgCl₂,Mg(ClO₃)₂, MgI₂, Mg(IO₃)₂, Mg(NO₂)₂, Mg(NO₃)₂, MgSO₃, MgSO₄, MgS₂O₆,Mg(CH₃COO)₂, Mg(OH)₂, and Mg(ClO₄)₂; and Sr salts such as SrBr₂, SrCl₂,SrI₂, Sr(NO₃)₂, SrO, SrS₂O₃, SrS₂O₆, SrS₄O₆, Sr(CH₃COO)₂, and Sr(OH)₂.These compounds may be used singly or in combination or two or morespecies.

The amount of the aforementioned component (d); i.e., at least onecomponent selected from among a ruthenium component, a platinumcomponent, a rhodium component, a palladium component, and an iridiumcomponent, supported on the carrier, is generally 0.1 to 8 mass %, asreduced to noble metal element(s) and based on the reforming catalyst,preferably 0.5 to 5 mass %.

The lanthanum oxide content, the cerium oxide content, or the zirconiumoxide content of the reforming catalyst is preferably 1 to 20 mass %,more preferably 2.5 to 10 mass %.

The silicon oxide content is preferably 1 to 20 mass % based on thereforming catalyst, more preferably 2.5 to 10 mass %.

After completion of the above supporting operation, the catalyst isdried in accordance with needs. Examples of the drying method includenatural drying and drying by use of a rotary evaporator or a blowerdryer.

No particular limitation is imposed on the shape or size of thereforming catalyst prepared in the invention, and reforming catalysts inthe form of powder, balls, particles, honeycomb structure, foam, fiber,cloth, plate, ring, etc., which are generally employed, may be selected.

After the thus-prepared catalyst has been charged into a reformer, thecatalyst is subjected to reduction with hydrogen. The reductiontreatment is performed through gas phase reduction in gas flowcontaining hydrogen, or through wet-format reduction by use of areducing agent. The former gas phase reduction is generally performed ina gas flow containing hydrogen at 500 to 800° C., preferably 600 to 700°C., for 1 to 24 hours, preferably 3 to 12 hours.

Examples of the latter wet-format reduction include Birch reduction,which employs liquid ammonia/alcohol/Na or liquid ammonia/alcohol/Li;Benkeser reduction, which employs methylamine/Li or a similar system;and reduction methods employing a reducing agent such as Zn/HCl,Al/NaOH/H₂O, NaH, LiAlH₄ or a substituted compound, hydrosilanes, sodiumborohydride or a substituted compound, diborane, formic acid, formalin,or hydrazines. In this case, reduction is generally carried out at roomtemperature to 100° C. for 10 minutes to 24 hours, preferably 30 minutesto 10 hours.

The method for reforming hydrocarbon by use of the reforming catalyst ofthe present invention will next be described.

Firstly, steam reforming reaction of hydrocarbon in the presence of thereforming catalyst of the present invention will be described.

Examples of hydrocarbon feedstocks employed in the steam reformingreaction include linear-chain or branched saturated aliphatichydrocarbons having about 1 to 16 carbon atoms such as methane, ethane,propane, butane, pentane, hexane, heptane, octane, nonane, and decane;saturated alicyclic hydrocarbons such as cyclohexane, methylcyclohexane,and cyclooctane; monocyclic and polycyclic aromatic hydrocarbons; citygas, LPG, naphtha, and kerosene.

Generally, when such a hydrocarbon feedstock contains sulfur, thematerial is preferably desulfurized to a sulfur content of 0.1 ppm orless through a desulfurization step. When the sulfur content of thehydrocarbon feedstock is in excess of about 0.1 ppm, a steam reformingcatalyst may be deactivated. No particular limitation is imposed on thedesulfurization method, and any desulfurization method such ashydrogenation desulfurization or adsorption desulfurization may beappropriately employed. Needless to say, no particular limitation isimposed on the steam which is employed in steam reforming.

In determination of steam reforming reaction conditions, the amount ofhydrocarbon and that of steam are controlled such that the steam/carbon(mol) ratio is generally regulated to 1.5 to 10, preferably 1.5 to 5,more preferably 2 to 4. Through control of the steam/carbon (mol) ratio,hydrogen gas can be yielded efficiently.

The reaction temperature is generally 200 to 900° C., preferably 250 to900° C., more preferably 300 to 800° C. The reaction pressure isgenerally 0 to 3 MPa·G, preferably 0 to 1 MPa·G.

When a hydrocarbon having a boiling point equal to or higher than thatof kerosene is employed as a feedstock, steam reforming is preferablyperformed while the inlet temperature of a steam reforming catalystlayer is maintained at 630° C. or lower; preferably 600° C. or lower.When the inlet temperature is higher than 630° C., pyrolysis of thehydrocarbon is promoted, to thereby form radicals, and carbon isdeposited on the catalyst or the reactor tube wall, leading in somecases to difficulty in operation. No particular limitation is imposed onthe outlet temperature of the catalyst layer, but the outlet temperaturepreferably falls within a range of 650 to 800° C. When the outlettemperature is lower than 650° C., the amount of formed hydrogen may beunsatisfactory, whereas when the temperature is higher than 800° C., thereactor may require heat resistant materials, hence economicallyunfavorable.

In the above case, a somewhat larger amount of steam is fed, and thereaction temperature and the reaction pressure are both somewhat low.

Secondary, autothermal reforming reaction, partial-oxidation reformingreaction, and carbon dioxide reforming reaction of hydrocarbon, by useof the reforming catalyst of the present invention, will be described.

In the autothermal reforming, oxidation of a hydrocarbon and reaction ofa hydrocarbon with steam occur in the same reactor or continuouslydisposed reactors. In the production of hydrogen, the reactiontemperature is generally 200 to 1,300° C., preferably 400 to 1,200° C.,more preferably 500 to 900° C.; the steam/carbon (mol) ratio isgenerally 0.1 to 10, preferably 0.4 to 4; the oxygen/carbon (mol) ratiois generally 0.1 to 1, preferably 0.2 to 0.8; and the reaction pressureis generally 0 to 10 MPa·G, preferably 0 to 5 MPa·G, more preferably 0to 3 MPa·G. Hydrocarbons similar to those employed in steam reformingare used in autothermal reforming.

In the partial-oxidation reforming, partial oxidation of a hydrocarbonoccurs. In the production of hydrogen, the reaction temperature isgenerally 350 to 1,200° C., preferably 450 to 900° C.; the oxygen/carbon(mol) ratio is generally 0.4 to 0.8, preferably 0.45 to 0.65; and thereaction pressure is generally 0 to 30 MPa·G, preferably 0 to 5 MPa·G,more preferably 0 to 3 MPa·G. Hydrocarbons similar to those employed insteam reforming are used in partial-oxidation reforming.

In the carbon dioxide reforming, reaction of a hydrocarbon with carbondioxide occurs. In the production of hydrogen, the reaction temperatureis generally 200 to 1,300° C., preferably 400 to 1,200° C., morepreferably 500 to 900° C.; the carbon dioxide/carbon (mol) ratio isgenerally 0.1 to 5, preferably 0.1 to 3; the steam/carbon (mol) ratio(when steam is fed) is generally 0.1 to 10, preferably 0.4 to 4; theoxygen/carbon (mol) ratio (when oxygen is fed) is generally 0.1 to 1,preferably 0.2 to 0.8; and the reaction pressure is generally 0 to 10MPa·G, preferably 0 to 5 MPa·G, more preferably 0 to 3 MPa·G. Althoughmethane is typically used as the hydrocarbon, other hydrocarbons similarto those employed in steam reforming are also used in carbon dioxidereforming.

The aforementioned reforming reactions may be performed in a continuousflow manner or in a batch manner, with a continuous flow manner beingpreferred. When the continuous flow manner is employed, liquid hourlyspace velocity (LHSV) of hydrocarbon is generally 0.1 to 10 hr⁻¹,preferably 0.25 to 5 hr⁻¹, whereas when hydrocarbon gas such as methaneis employed, gas hourly space velocity (GHSV) of the gas is generally200 to 100,000 hr⁻¹.

No particular limitation is imposed on the reaction type, and any of afixed-bed type, a moving-bed type, and a fluidizing-bed type can beemployed, with a fixed-bed type being preferred. No particularlimitation is imposed on the reactor type, and reactors such as a tubereactor can be employed.

Through use of the reforming catalyst of the present invention under theaforementioned conditions, a hydrocarbon is subjected to steamreforming, autothermal reforming, partial-oxidation reforming, or carbondioxide reforming, to thereby yield hydrogen. Such a reforming issuitably employed as a process for producing hydrogen for use in a fuelcell.

A characteristic feature of the fuel cell system of the presentinvention is that the fuel cell system includes a reformer employing theaforementioned reforming catalyst, and a fuel cell employing, as a fuel,hydrogen produced by the reformer. An embodiment of the fuel cell systemwill next be described with reference to FIG. 1.

A fuel placed in a fuel tank 21 is transferred to a desulfurizer 23through a fuel pump 22. An adsorbent such as activated carbon, zeolite,or a metallic adsorbent may be charged into the desulfurizer 23. Thefuel which has been desulfurized by means of the desulfurizer 23intermingles with water fed from a water tank through a water pump 24,and the mixture is fed to a vaporizer 1, where the mixture is vaporized.Subsequently, the vapor is mixed with air fed through an air blower 35,and the gas stream is transferred to a reformer 31, where theaforementioned reforming catalyst is charged. Hydrogen is produced fromthe fuel mixture (gas mixture containing hydrocarbon, steam, and oxygen)which is transferred to reformer 31, according to any of theaforementioned reforming processes.

CO content of the thus-produced hydrogen is lowered, through a shiftreactor of carbon monoxide 32 and a preferential oxidation reactor ofcarbon monoxide, to such a level that the characteristics of the fuelcell are not impaired. Examples of the catalyst employed in the shiftreactor of carbon monoxide 32 include an iron-chromium catalyst, acopper-zinc catalyst, and a noble metal catalyst. Examples of thecatalyst employed in the preferential oxidation reactor of carbonmonoxide 33 include a ruthenium catalyst, a platinum catalyst, and amixture thereof. In the case where hydrogen produced through reforminghas a low CO content, the shift reactor of carbon monoxide 32 and thepreferential oxidation reactor of carbon monoxide 33 are not required.

A fuel cell 34, which is a type of a polymer electrolyte fuel cell,includes a negative electrode 34A, a positive electrode 34B, and polymerelectrolyte 34C provided between the electrodes. A hydrogen-rich gasproduced through the above method is fed to the negative electrode, andair supplied by the air blower 35 is fed to the positive electrode.These two gases are appropriately humidified (humidifier notillustrated) in accordance with needs before introduction to theelectrodes.

In operation, hydrogen gas releases electrons, thereby generatingprotons in the negative electrode, and oxygen gas forms water bycapturing electrons and protons in the positive electrode, wherebydirect current is generated between the electrodes 34A and 34B. In thiscase, the negative electrode is a platinum or Pt—Ru-alloy catalystsupporting platinum black or activated carbon, or a similar material,and the positive electrode is a platinum catalyst supporting platinumblack or activated carbon, or a similar material.

An excessive amount of hydrogen serves as a fuel, when a burner 31A ofthe reformer 31 is connected to the negative electrode 34A. When agas-water separator 36 is connected to the positive electrode 34B, waterwhich has been formed through combination of hydrogen, and oxygenpresent in the air fed to the positive electrode 34B can be separatedfrom the discharge gas. The thus-separated water can be utilized as asource of steam. Since the fuel cell 34 generates heat in the course ofpower generation, an exhaust heat recovery unit 37 is provided so as torecover and effectively utilize the heat. The exhaust heat recovery unit37 includes a heat exchanger 37A attached to the fuel cell 34 forabsorbing heat generated during reaction; a heat exchanger 37B forexchanging the heat absorbed by the heat exchanger 37A with water; acooling unit 37C; and a pump 37D for circulating a cooling medium in theheat exchangers 37A and 37B and the cooling unit 37C. Warm waterobtained in the heat exchanger 37B may be effectively utilized in otherfacilities.

EXAMPLES

The present invention will next be described in more detail by way ofexamples, which should not be construed as limiting the inventionthereto.

(1) Compressive strength of each catalyst sample was determined by meansof a Kiya-type strength meter (in accordance with ASTM D4179).

(2) Catalytic activity was obtained from C1 percent conversion (i.e.,percent conversion to C1 species) (%) determined through the followingprocedure.

Each catalyst sample was pulverized to a particle size of 0.5 to 1 mm.The catalyst powder (1.5 mL) and SiC (3.5 mL) were charged into areformer. The catalyst in the reformer was reduced with hydrogen in ahydrogen flow at 600° C. for one hour. Subsequently, steam reformingreaction was performed in the presence of the catalyst (accelerateddeterioration test). Commercial kerosene (JIS No. 1) desulfurized tohave a sulfur content of 0.01 ppm or less was used as a hydrocarbonfeedstock. The feedstock (kerosene) and steam were introduced to thereformer at an LHSV of 4.6 hr⁻¹ and a steam/carbon (mole ratio) of 1.5and at atmospheric pressure and a reaction temperature (center of thecatalyst layer) of 600° C. After five hours from initiation ofreforming, the gas obtained was sampled and analyzed through gaschromatography in terms of component and concentration. From theanalytical data, C1 percent conversion was calculated by the followingequation:C1 percent conversion (%)=(A/B)×100(wherein A is a sum of flow rate of CO (mol)+flow rate of CO₂ (mol)+flowrate of CH₄ (mol) (flow rate at the reactor outlet) and B representsflow rate of kerosene (mol, as reduced to carbon) at the reactor inlet).(3) Steam Treatment Test (1)

Each catalyst sample was pulverized to a particle size of 0.5 to 1 mm.The catalyst powder (5 mL) was charged into a micro-reactor (innerdiameter: 20 mm). To the reactor filled with the catalyst, H₂ (200NmL/min) and H₂O (0.132 g/min) were fed so as to perform steam treatmentof the catalyst at 800° C. for five hours.

(3) Steam Treatment Test (2)

Each catalyst sample was pulverized to a particle size of 0.5 to 1 mm.The catalyst powder (5 mL) was charged into a micro-reactor. To thereactor filled with the catalyst, H₂ (200 NmL/min) and H₂O (1.019 g/min)were fed so as to perform steam treatment of the catalyst at 850° C. for96 hours.

(4) Evaluation of Heat Resistance

Each catalyst sample was calcined in a muffle furnace at 950° C. for 12hours. Surface area and compressive strength of each sample before andafter calcining were determined, whereby heat resistance of the samplewas evaluated.

The surface area of each catalyst sample was determined through thesurface area measurement (nitrogen adsorption) BET one-point method.

Example 1 Preparation of 3Ru/6MnO₂(A)/5La₂O₃/KHO-24 (Catalyst 1),Wherein (A) Indicates that the Component is Formed from a CorrespondingAcetate Salt

(i) Lanthanum nitrate (La(NO₃)₃.6H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (2.82 g) was dissolved in water (7.1 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 500° C. for three hours, to thereby prepare an aluminacarrier containing 5 mass % lanthanum oxide.

(iii) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (6.2 mL), and thealumina carrier containing lanthanum oxide obtained in (ii) above (20 g)was impregnated with the solution.

(iv) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 800° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide and 5 mass % lanthanumoxide.

(v) Ruthenium chloride (RuCl₃, product of Tanaka Kikinzoku Kogyo K.K.;Ru content: 39.9 mass %) (1.55 g) was dissolved in water (7.8 mL), andthe carrier prepared in (iv) above was impregnated with rutheniumchloride by use of the solution.

(vi) After completion of impregnation, the carrier was left to stand forabout 30 minutes and dried, to thereby produce a crude catalyst.

(vii) The crude catalyst obtained in (vi) above was immersed in a 5mol/L sodium hydroxide solution (25 mL) for one hour so as to carry outimpregnation, whereby the above compounds were decomposed.

(viii) Subsequently, the thus-treated catalyst was sufficiently washedwith distilled water and dried by means of a dryer at 120° C. for threehours, whereby catalyst 1 was prepared.

The thus-prepared catalyst was found to have a Ru content of 3.0 mass %.

Example 2 Preparation of 3Ru/5La₂O₃/6MnO₂(A)/KHO-24 (Catalyst 2),Wherein (A) Indicates that the Component is Formed from a CorrespondingAcetate Salt

(i) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (7.5 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 800° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide.

(iii) Lanthanum nitrate (La(NO₃)₃.6H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (2.82 g) was dissolved in water (6.2 mL), and thealumina carrier containing manganese oxide obtained in (ii) above (20 g)was impregnated with the solution.

(iv) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 800° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide and 5 mass % lanthanumoxide.

(v) Subsequently, the same procedure as employed in (v) to (viii) ofExample 1 (preparation of catalyst 1) was repeated, whereby catalyst 2was prepared.

Example 3 Preparation of 3Ru/6MnO₂(A)+5La₂O₃/KHO-24 (Catalyst 3),Wherein (A) Indicates that the Component is Formed from a CorrespondingAcetate Salt

(i) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) and lanthanum nitrate (La(NO₃)₃.6H₂O, productof Wako Pure Chemical Industries, Ltd.) (2.82 g) were simultaneouslydissolved in water (6.3 mL), and γ-alumina (KHO-24, product of SumitomoChemical Co., Ltd.) (20 g) was impregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 800° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide and 5 mass % lanthanumoxide.

(iii) Subsequently, the same procedure as employed in (v) to (viii) ofExample 1 (preparation of catalyst 1) was repeated, whereby catalyst 3was prepared.

Example 4 Preparation of 3Ru/6MnO₂(A)/5La₂O₃/KHO-24 (Catalyst 4),Wherein (A) Indicates that the Component is Formed from a CorrespondingAcetate Salt

(i) Lanthanum nitrate (La(NO₃)₃.6H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (2.82 g) was dissolved in water (7.1 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 500° C. for three hours, to thereby prepare an aluminacarrier containing 5 mass % lanthanum oxide.

(iii) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (6.2 mL), and thealumina carrier containing lanthanum oxide obtained in (ii) above (20 g)was impregnated with the solution.

(iv) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 950° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide and 5 mass % lanthanumoxide.

(v) Subsequently, the same procedure as employed in (v) to (viii) ofExample 1 (preparation of catalyst 1) was repeated, whereby catalyst 4was prepared.

Example 5 Preparation of 3Ru/10MnO₂(N)/5La₂O₃/KHO-24 (Catalyst 5),Wherein (N) Indicates that the Component is Formed from a CorrespondingNitrate Salt

(i) Lanthanum nitrate (La(NO₃)₃.6H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (2.82 g) was dissolved in water (7.1 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 500° C. for three hours, to thereby prepare an aluminacarrier containing 5 mass % lanthanum oxide.

(iii) Manganese nitrate (Mn(NO₃)₂.6H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (7.41 g) was dissolved in water (6.2 mL), and thealumina carrier containing lanthanum oxide obtained in (ii) above (20 g)was impregnated with the solution.

(iv) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 950° C. for three hours, to thereby prepare an aluminacarrier containing 10 mass % manganese oxide and 5 mass % lanthanumoxide.

(v) Subsequently, the same procedure as employed in (v) to (viii) ofExample 1 (preparation of catalyst 1) was repeated, whereby catalyst 5was prepared.

The thus-prepared catalyst was found to have an Ru content of 3.0 mass%.

Example 6 Preparation of 3Ru/6MnO₂(A)/5CeO₂/KHO-24 (Catalyst 6), Wherein(A) Indicates that the Component is Formed from a Corresponding AcetateSalt

(i) Cerium nitrate (Ce(NO₃)₃.6H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (2.71 g) was dissolved in water (7.1 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 500° C. for three hours, to thereby prepare an aluminacarrier containing 5 mass % cerium oxide.

(iii) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (6.2 mL), and thealumina carrier containing cerium oxide obtained in (ii) above (20 g)was impregnated with the solution.

(iv) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 800° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide and 5 mass % cerium oxide.

(v) Subsequently, the same procedure as employed in (v) to (viii) ofExample 1 (preparation of catalyst 1) was repeated, whereby catalyst 6was prepared.

The thus-prepared catalyst was found to have an Ru content of 3.0 mass%.

Example 7 Preparation of 3Ru/6MnO₂(A)/5ZrO₂/KHO-24 (Catalyst 7), Wherein(A) Indicates that the Component is Formed from a Corresponding AcetateSalt

(i) Zirconium nitrate (Zr(NO₃)₂.2H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (2.33 g) was dissolved in water (6.9 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 500° C. for three hours, to thereby prepare an aluminacarrier containing 5 mass % zirconium oxide.

(iii) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (6.2 mL), and thealumina carrier containing zirconium oxide prepared in (ii) above (20 g)was impregnated with the solution.

(iv) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 800° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide and 5 mass % zirconiumoxide.

(v) Subsequently, the same procedure as employed in (v) to (viii) ofExample 1 (preparation of catalyst 1) was repeated, whereby catalyst 7was prepared.

The thus-prepared catalyst was found to have a Ru content of 3.0 mass %.

Comparative Example 1 Preparation of 3Ru-6MnO₂/KHO-24 (Catalyst 8)

(i) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (7.5 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution.

(ii) Subsequently, the impregnation product was dried by means of adryer at 120° C. for three hours, followed by calcining in a mufflefurnace at 500° C. for three hours, to thereby prepare an aluminacarrier containing 6 mass % manganese oxide.

(iii) Ruthenium chloride (RuCl₃, product of Tanaka Kikinzoku kogyo K.K.;Ru content: 39.9 mass %) (1.55 g) was dissolved in water (7.8 mL), andthe carrier prepared in (ii) above was impregnated with rutheniumchloride by use of the solution. Subsequently, the carrier was dried bymeans of a dryer at 80° C. for three hours.

(iv) The thus-dried carrier was immersed in a 5 mol/L sodium hydroxidesolution (25 mL) for one hour so as to carry out impregnation, wherebythe above compounds were decomposed.

(v) Subsequently, the thus-treated catalyst was sufficiently washed withdistilled water and dried by means of a dryer at 120° C. for threehours, whereby catalyst 8 was prepared.

The thus-prepared catalyst was found to have a Ru content of 3.0 mass %.

Test Example 1

Each of the catalysts produced in Examples 1 to 7 and ComparativeExample 1 was evaluated. Specifically, percent conversion to C1 species(C1 percent conversion) was determined so as to evaluate catalyticactivity and the catalyst was subjected to steam treatment tests (1) and(2). After completion of each steam treatment test, mechanical strengthof the catalyst was measured, and C1 percent conversion was determinedunder the same conditions so as to evaluate catalytic activity. Theresults are shown in Table 1.

TABLE 1 Compressive strength Catalyst Catalyst (kg) after Activity (%)Compressive Calcining- compressive CO steam after steam strength (kg)Activity (%) La Mn temp. Activity strength adsorption treatmenttreatment after steam after steam (mass %) (mass %) (° C.) (%) (kg)(μmol/g) (1) (1) treatment (2) treatment (2) Ex. 1 Catalyst 1 5 from 80078.2 18 67.1 15 68.3 10 26.7 acetate (6) Ex. 2 Catalyst 2 5 from 80073.4 19 72.9 15 66.2 10 24.3 acetate (6) Ex. 3 Catalyst 3 5 from 80073.7 23 72.4 15.5 68.2 10 22.7 acetate (6) Ex. 4 Catalyst 4 5 from 95071.1 16 76.6 15 65.3 5 18.5 acetate (6) Ex. 5 Catalyst 5 5 from 950 71.614 65.7 13 65.2 4 18.2 acetate (10) Ex. 6 Catalyst 6 Ce 5 from 800 71.518 65.0 15 61.6 7 18.4 acetate (6) Ex. 7 Catalyst 7 Zr 5 from 800 66.318 62.0 15 58.3 7 18.3 acetate (6) Comp. Catalyst 8 — from 800 61.5 1756.2 14 55.1 2.5 11.8 Ex. 1 acetate (6)

Comparative Example 2 Preparation of 3Ru/KHO-24 (Catalyst 9)

(i) Ruthenium chloride (RuCl₃, product of Tanaka Kikinzoku kogyo k. k.;Ru content: 39.9 mass %) (1.55 g) was dissolved in water (7.8 mL), andγ-alumina (KHO-24, commercial product of Sumitomo Chemical Co., Ltd.)was impregnated with the aqueous ruthenium chloride solution. Aftercompletion of impregnation, the carrier was left to stand for about 30minutes, to thereby produce a crude catalyst. The thus-obtained crudecatalyst was immersed in a 5 mol/L sodium hydroxide solution (25 mL) forone hour so as to carry out impregnation, whereby the Ru compound wasdecomposed. Subsequently, the thus-treated catalyst was sufficientlywashed with distilled water and dried by means of a dryer at 120° C. forthree hours, whereby catalyst 9 was prepared.

Example 8 Preparation of 3Ru/6MnO₂(A)/3SiO₂/KHO-24 (Catalyst 10),Wherein (A) Indicates that the Component is Formed from a CorrespondingAcetate Salt

(i) Tetraethoxysilane (Si(OC₂H₅)₄, product of Shin-Etsu Chemical Co.,Ltd.) (4.60 g) was dissolved in ethanol (100 mL), and γ-alumina (KHO-24,product of Sumitomo Chemical Co., Ltd.) (20 g) was immersed in thesolution. The mixture was allowed to react at 60° C. for one hour understirring. After completion of reaction, ethanol was removed by means ofa rotary evaporator, and the reaction mixture was dried overnight bymeans of a dryer at 120° C. The dried product was calcined in a mufflefurnace at 800° C. for three hours, to thereby prepare an aluminacarrier containing 3 mass % silicon oxide (3SiO₂/KHO-24). Subsequently,manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (7.5 mL), and theabove alumina carrier containing 3 mass % silicon oxide (3SiO₂/KHO-24)was impregnated with the solution. The impregnation product was calcinedin a muffle furnace at 800° C. for three hours, to thereby prepare analumina carrier containing manganese oxide and silicon oxide(6MnO₂(A)/3SiO₂/KHO-24).

(ii) Ruthenium chloride (RuCl₃, product of Tanaka Kikinzoku Kogyo K.K.;Ru content: 39.9 mass %) (1.55 g) was dissolved in water (7.8 mL), andthe alumina carrier containing manganese oxide and silicon oxideprepared above was impregnated with the aqueous ruthenium chloridesolution. After completion of impregnation, the carrier was left tostand for about 30 minutes for drying, to thereby produce a crudecatalyst. The crude catalyst obtained above was immersed in a 5 mol/Lsodium hydroxide solution (25 mL) for one hour so as to carry outimpregnation, whereby the above compounds were decomposed. Subsequently,the thus-treated catalyst was sufficiently washed with distilled waterand dried by means of a dryer at 120° C. for three hours, wherebycatalyst 10 was prepared.

The thus-prepared catalyst was found to have a Ru content of 3.0 mass %.

Example 9 Preparation of 3Ru/3SiO₂/6MnO₂(A)/KHO-24 (Catalyst 11),Wherein (A) Indicates that the Component is Formed from a CorrespondingAcetate Salt

(i) Manganese acetate (Mn(CH₃COO)₂.4H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (3.64 g) was dissolved in water (7.5 mL), and aluminawas impregnated with the solution. Subsequently, the impregnationproduct was dried by means of a dryer at 120° C. for three hours,followed by calcining in a muffle furnace at 800° C. for three hours, tothereby prepare an alumina carrier containing manganese oxide(6MnO₂/KHO-24) Tetraethoxysilane (Si(OC₂H₅)₄, product of Shin-EtsuChemical Co., Ltd.) (4.60 g) was dissolved in ethanol (100 mL), and theabove-prepared alumina carrier containing manganese oxide (20 g) wasimmersed in the solution. The mixture was allowed to react at 60° C. forone hour under stirring. After completion of reaction, ethanol wasremoved by means of a rotary evaporator, and the reaction mixture wasdried overnight by means of a dryer at 120° C. The dried product wascalcined in a muffle furnace at 800° C. for three hours, to therebyprepare an alumina carrier containing 3 mass % silicon oxide andmanganese oxide (3SiO₂/6MnO₂/KHO-24).

(ii) The same procedure as employed in (ii) of Example 8 was repeated,except that the above-produced alumina carrier containing 3 mass %silicon oxide and manganese oxide (3SiO₂/6MnO₂(A)/KHO-24) was employed,whereby catalyst 11 was prepared.

The thus-prepared catalyst was found to have a Ru content of 3.0 mass %.

Comparative Example 3 Preparation of 3Ru/5La₂O₃(N)/KHO-24 (Catalyst 12),Wherein (N) Indicates that the Component is Formed from a CorrespondingNitrate Salt

(i) Lanthanum nitrate (La(NO₃)₃.6H₂O, product of Wako Pure ChemicalIndustries, Ltd.) (2.82 g) was dissolved in water (7.1 mL), andγ-alumina (KHO-24, product of Sumitomo Chemical Co., Ltd.) (20 g) wasimpregnated with the solution. Subsequently, the impregnation productwas dried by means of a dryer at 120° C. for three hours, followed bycalcining in a muffle furnace at 800° C. for three hours, to therebyprepare an alumina carrier containing 5 mass % lanthanum oxide.

(ii) The same procedure as employed in (ii) of Example 8 was repeated,except that the above-produced alumina carrier containing 5 mass %lanthanum oxide was employed, whereby catalyst 12 was prepared.

Test Example 2

Each of the catalysts produced in Examples 8 and 9 and ComparativeExamples 2 and 3 was evaluated in terms of heat resistance. The resultsare shown in Table 2.

TABLE 2 Before calcining After calcining at 950° C. at 950° C. SurfaceSurface area Compressive area Compressive Catalyst (m²/g) strength (kg)(m²/g) strength (kg) Comp. Catalyst 9 149 18 70 13 Ex. 2 Ex. 8 Catalyst10 117 14 100 18 Ex. 9 Catalyst 11 119 15 104 18 Comp. Catalyst 12 12019 88 17 Ex. 3

INDUSTRIAL APPLICABILITY

According to the present invention, there can be provided a hydrocarbonreforming catalyst which maintains carrier strength (particularly,compressive strength of the carrier) even after a long-term thermalhistory, which exhibits high catalytic activity, and which maintains thecatalytic activity even after a long-term thermal history; a hydrocarbonreforming catalyst which exhibits enhanced heat resistance; and a methodfor producing hydrogen by use of any of the reforming catalysts. Theinvention can also provide an advanced fuel cell system comprising areformer employing such an excellent reforming catalyst, and a fuel cellemploying, as a fuel, hydrogen produced by the reformer.

1. A hydrocarbon reforming catalyst, comprising: a carrier consisting of(a), (b), and (c); wherein (a) is at least one compound selected fromthe group consisting of lanthanum oxide, cerium oxide, and zirconiumoxide; (b) is manganese oxide; (c) is alumina; and (d), supported on thecarrier, at least one noble metal component selected from the groupconsisting of a ruthenium component, a platinum component, a rhodiumcomponent, a palladium component, and an iridium component; whereincomponent (a) of the carrier is present in an amount of 1 to 20 mass %with respect to the amount of the reforming catalyst; wherein the noblemetal component is present in an amount of 0.1 to 8 mass % as reduced tothe noble metal element based on the amount of the reforming catalyst;and wherein the carrier is produced by impregnating alumina with atleast one compound selected from the group consisting of a lanthanumcompound, a cerium compound, and a zirconium compound; calcining theimpregnated alumina carrier at 400 to 600° C.; impregnating the calcinedalumina carrier with a manganese compound; and calcining the manganeseimpregnated calcined alumina carrier at 800 to 1,000° C.
 2. Thehydrocarbon reforming catalyst as described in claim 1, wherein themanganese compound is manganese acetate.
 3. The hydrocarbon reformingcatalyst as described in claim 1, wherein the manganese oxide iscontained in the reforming catalyst in an amount of 3 to 20 mass %. 4.The hydrocarbon reforming catalyst as described in claim 1, whichfurther contains at least one species selected from the group consistingof an alkali metal component and an alkaline earth metal component.
 5. Amethod for producing hydrogen comprising reforming a hydrocarbon bycontacting the hydrocarbon with the reforming catalyst as recited inclaim
 1. 6. The method for producing hydrogen as described in claim 5,wherein the reforming is steam reforming, autothermal reforming,partial-oxidation reforming, or carbon dioxide reforming.
 7. A fuel cellsystem comprising a reformer employing a reforming catalyst as recitedin claim 1, and a fuel cell employing, as a fuel, hydrogen produced bysaid reformer.
 8. A hydrocarbon reforming catalyst, consisting ofcomponents (a), (b), (c) and (d): wherein (a), (b), and (c) arecomponents of a carrier (a) is at least one compound selected from thegroup consisting of lanthanum oxide, cerium oxide, and zirconium oxide,(b) is manganese oxide, (c) is alumina, and (d), supported on thecarrier, at least one noble metal component selected from the groupconsisting of a ruthenium component, a platinum component, a rhodiumcomponent, a palladium component, and an iridium component; whereincomponent (a) of the carrier is present in an amount of 1 to 20 mass %with respect to the amount of the reforming catalyst; and wherein thenoble metal component is present in an amount of 0.1 to 8 mass % asreduced to the noble metal element based on the amount of the reformingcatalyst.
 9. A hydrocarbon reforming catalyst, comprising: a carrierconsisting of (a) lanthanum oxide, (b) manganese oxide, and (c) alumina,and (d), supported on the carrier, at least one noble metal componentselected from the group consisting of a ruthenium component, a platinumcomponent, a rhodium component, a palladium component, and an iridiumcomponent; wherein component (a) of the carrier is present in an amountof 1 to 20 mass % with respect to the amount of the reforming catalyst;and wherein the noble metal component is present in an amount of 0.1 to8 mass % as reduced to the noble metal element based on the amount ofthe reforming catalyst.